Hydrogenation of aromatics with a tungsten and nickel sulfide, supported on alumina, catalyst composite



United States Patent() HYDROGENATION OF AROMATICS WITH A TUNGSTEN AND NICKEL SULFIDE, -SUP- POgTED ON ALUMINA, CATALYST COM- PO ITE No Drawing. Filed Aug. 4, 1958, Ser. No. 753,109

2 Claims. (Cl. 260-667) This invention relates to catalysts and processes for the saturative hydrogenation of aromatics existing either alone or in admixture with other substances.

Many hydrocarbon stocks, such as jet fuels, diesel fuels, gas turbine fuels, kerosenes, furnace oils, lubricating oils, etc., can be upgraded by the saturative hydrogenationof the aromatic constituents they contain. For example, furnace oil distillates from cracking processes usually contain a relatively large percentage of aromatic compounds, in addition to having relatively high sulfur and olefin contents. Although the common commercial hydrogen refining processes result in considerable improvement in the quality of these oils, including removal of sulfur and hydrogenation of olefins, their aromatic contents remain substantially unchanged. Since aromatic compounds in general have poor burning characteristics, conversion of the aromatics in such cracked distillates to the corresponding naphthenes is desirable for further improvement in quality. In the case of jet fuels, it is desirable to convert aromatic compounds to the corresponding naphthenes because of the higher heats of combustion of the saturated compounds. Accordingly, this invention is directed to the saturative hydrogenation of aromatics. By the term saturative hydrogenation of aromatics We refer to the addition of hydrogen to the aromatic portions of a molecule rather than the addition of hydrogen to olefinic portions of a molecule, although the two may occur concomitantly.

According to this invention, extremely high conversions in the saturative hydrogenation of aromatics are achieved by passing an aromatic containing material and hydrogen at a temperature of 550 to 850 F. generally and 650 to 750 F. preferably and at a pressure of 500 to 4000 pounds per square inch gauge over a catalyst comprising the oxides or sulfides of tungsten and an oxide or sulfide of at least one metal selected from group VIII. The preferable group VIII metals are iron, cobalt and nickel, generally and the most preferable group VIII metal is nickel. The catalyst may be supported or unsupported, but is preferably disposed upon a suitable supporting ma- 'ice supports are alumina, silica, magnesia, zirconia, kieselguhr, pumice, etc. In the supported catalysts of this invention, the active metals can be present either in the oxide form or they can be at least partially sulfided. Since the conversion of certain oxides, particularly those of tungsten, to the corresponding sulfides proceeds very slowly a sulfiding treatment of any reasonable length does not convert the oxides completely to sulfides. The product of a sulfiding treatment of metal oxides is generally a mixture of sulfides, oxides, oxysulfides, free metals and free sulfur.

The optimum total active metals content in the supported catalysts will be dependent upon whether these metals are present in the oxided or sulfided state. The supported oxided catalyst has a different optimum metals content than the supported sulfided form. The oxide catalyst should contain 5 to 40 percent metals by weight generally, expressed as pure metals, and preferably between 20 and 28 percent metals. When the catalyst is employed in the sulfided state, it should contain 5 to 40 percent metals by weight generally and preferably it should contain 10 to percent metals. In the case of both the oxided and sulfided supported catalysts, as well as for the unsupported catalysts, the atomic ratio of tung sten to group VIII metal should be 0.2:1 to 5 .0:1 generally, but the preferable ratio is 0.8:1 to 1.2: l. The sulfided supported catalysts of this invention can contain between 0.5 and 15 percent sulfur by weight. The unsupported catalyst of this invention can be prepared by any suitable method. For example, a solution of ammonium sulfide and the ammonium thio salt of a group VI element is prepared by treating an ammoniacal solution of an ammonium salt of a group VI metal with hydrogen sulfide. A group VIII salt is then added to this solution to obtain a group VIII metal sulfide precipitate. Following this the group VI metal sulfide is precipitated by acidifying the medium. Thereafter the mixed sulfides are recovered and subjected to reducing conditions and then converted into a form suitable as a catalyst.

In the preparation of the supported catalyst composi tions of this invention, the carriermaterial is impregnated with one or more solutions containing soluble compounds of the active metals, such as ammonium meta tungstate and nickel nitrate. The proportions of such soluble compounds placed in solution are adjusted to produce a catalyst containing the desired amount of metals and the desired ratio of metals to each other. Either single or multiple impregnation of the carrier with the solution or solutions containing the active metals can be employed. The preferable method of preparing the supported catalyst is by multiple impregnation wherein the tungsten is impregnated upon the support before the group VIII metal or metals. We have found that impregnating the.

- tungsten upon the support before the impregnation of the terial. Examples of materials suitable to be employed as v group VIII metal or metals produces a catalyst possessing superior activity in the saturative hydrogenation of aromatics. The impregnated support is then dried, calcined and preferablby sulfided;

The sulfiding step in the preparation of the supported catalysts of this invention is a solid phase reaction. The impregnated carrier can be treated with a gaseous or liquid sulfur containing substance, preferably in the presence of a reducing material such as hydrogen, by exposing the outer surface and pores of the impregnated carrier to the sulfur containing material. Hydrogen sulfide is the preferred sulfur containing material. Examples of other sulfur containing materials are methyl sulfide, propyl sulfide, ammonium sulfide, propyl mercaptan, etc. As explained above, the sulfiding treatment only partially converts the oxides to the sulfides and the product of the sulfiding step is a mixture of sulfides, oxides, oxysulfides and free sulfur.

If the supported catalyst is sulfided, the sulfiding operation should preferably employ a hydrogen sulfide containing mixture such as hydrogen-hydrogen sulfide com prising 1 to 99 volume percent hydrogen sulfide (measured at 60 'F. and atmospheric pressure) 'at a temperature of 500 to 750 F. for a duration of 2 to 20 hours. It is preferred that the sulfiding conditions should include a hydrogen-hydrogen sulfide containing mixturehaving a volumetric ratio of hydrogen to hydrogen sulfide of 2 to 12, a temperature of 600 to 700 F. and a sulfiding time duration of 4 to 12 hours.

Oxides or sulfides of group VI metals, generally, in combination with oxides or sulfides of group VIII metals are effective catalysts for the saturative hydrogenation of aromatic constituents. Such group VI metal containing catalysts are generally elfective for the saturation of aromatic constituents at temperatures of approximately 570 to 850 F. and pressures of about 300 pounds per square inch gauge. We have now discovered that when tungsten is chosen as the group VI metal in these catalysts, highly superior conversions are achieved by employing a hydrogenation pressure above 300 pounds per square inch gauge without any appreciable change in the temperature conditions. Generally, when tungsten containing catalysts are employed, greatly increased conversions are achieved by employing a pressure range of from 500 to 4000 pounds per square inch gauge. The surprising discovery has now been made that these greatly superior conversions are achieved by operating in this pressure range only when tungsten is present in the catalyst. In accordance with our invention, the beneficial effect accompanying an increase in hydrogenation pressure can best be achieved when employing a tungsten containing catalyst. Much less improvement in saturative hydrogenation activity is achieved at the elevated pressures of this invention when employing catalyst compositions containing other group VI metals in "place of tungsten.

The increased activity achieved when employing a tungsten containing catalyst of this invention at elevated pressures is illustrated in Table 1. Table 1 presents the activities of the catalysts tested for the saturation of aromatics in terms of a relative activity scale which was devised to conveniently compare the test data obtained by the use of various catalyst. This scale employs refractive index, n, as a measure of the aromatic content of a solution since the refractive index and aromatic content vary almost lineally over the range in which we are interested. Therefore, this scale of relative activity was devised so that a product having a refractive index equal to that of the charge was considered to have passed over a catalyst of activity and the same charge, when converted into a product having a refractive index corresponding to complete saturation of its aromatic content, was considered to have passed over a catalyst of activity 1000. Thus,

prrduct charire seturuted produce charge TABLE 1 The effect of pressure on saturation aczzvzty of several catalysts Catalyst Description Unsulfided Nil V Alumina Total Metals, Percent 25.64 Atomic Ratio 1.01 Ni:1.00 W Support.- Alcoa I-44 Alumina impregnation Techniq e (Vacuum) Single Charge- FCC F rnace Oil Distillate Conditions:

Hydrogen Rate, s.c.t./Bbl 3, 630 5, 000 Avg. Temperat'lre, F 70 701 Pressure, p.s.i.g 990 3, 020 Liquid Hourly Space Velocity,

Vol./Hr./Vol 1.12 1. 14 Throughput, Vol/Vol 22. 4 9. 1 Balance, Percent by Wt. of Charge:

Hydrocarbon Gases (C -C5) 0.3 0.1 Liquid 99. 2 97. 6 Sulfur removed... I 1. 5 1. 5

Total 101. 0 99. 2

Liquid Product Inspection:

Gravity API 24.3 31.7 34.7 Sulfur, GRM 1123, Percent 1. 55 0. 04 o. 04 Bromine N0.-

ASTM D 1159.....-.. 27. 7 1 0 FIA Analysis, Percent by Vol.

ASIM D 1319:

Olefins l4. 2 1.1 0.8 Aromatics-- 59. 5 .1. 3 14. 9 saturates 26. 3 57. 6 S4. 3 Aniline Point, F.-

ASTM D 611 83.2 111.8 145. J Distillation, Gas Oil- ASTM D 158:

Over Point, F 416 290 352 End Point, F. 640 600 620 467 430 426 494 464' 457 521 192 485 552 528 52.) 595 578 573 98. 5 98. 1 98. 0 Rcsid e, Percent 1. 3 1.3 5 Avg. No. Rings oer olecule- 1. 64 1. 58 1. 5:; Av g.N0. Aromatic Rings perm 0. 95 0. 46 0. 14 Refractive Index, 111,... l. 5169 1. 4822 1.4073 Catalyst Relative Activity 589 860 Catalyst Description"--. Tungsten-Nickel Sulfide Total Metals, Percent 19.9% Ni:43.3%

- /0 Atomic Ratio 1.44 NizLOO W Support Unsupported Impregnation Technique (Vacuum) Conditions:

Hydrogen Rate, s.c.f./Bbl 3, 900 3, 920 Avg. Temperature, F. 700 700 Pressure, p.s.i.g 1, 000 3,020 Liquid Hourly Space Velocity, V0l./Hr./V0l- 1. 04 0.98 Throughput, VOL/Vol 100. 3 19. 6

Balance, Percent by Wt. of Charge:

Hydrocarbon Gases-(CF03) 0.5 0. 9 Liquid 100. 1 100. 4 Sulfur Removed 2.0 1. 5

Total 102; 6 102. 8

Liquid Product Inspection Gravity, API.. 32. 9 37. 4 Sulfur, GRM 1123, Percen 0.08 0. 04 Bromine No. ASTM D 1159 3. 2 0.5

FIA Analysis, Percent by Vol.-

ASTM D 1319:

2. 5 3. 0 38.9 1.5 Saturates 58. 6 95, 5 Aniline Point, F.

ASTM D 611 115.0 161 o Distillation, Gas Oil- ASTM D 158:

Over Point F 328 352 End Point, F. 646 636 416 418 445 446 472 47G 507 514 570 570 Recovery, Percent. 98. 4 99. 0 Residue, Percent 1.1 1.0 Average No. Rings per molecule 1. 58 1. 60 Average No. Aromatic Rings per molecule 0.35 O. 00 Refractive Index, 11.0 1. 4763 1. 4580 Catalyst Relative Activity; 689 1, 000

ABLE 1C t' (I TABLE 1-Continued T on Catalyst Description Sulflded Sulfided- Catalyst Description Sulflded niw 1111] Total Metals, Percent 24.48 xg fi g rsktomictRatio 07 12 2 W 0m c 1 0 l 0 w upper coa umina Impregnation Technique (Vacuum) Single Support i fi gfi i fi 'g Impregnation Technique (Vacuum) oongflgnsz R t f/Bbl 3 820 4 340 v rogen a u Conditions: s;s-5$:? ;:ftgi{;jf;;; ,883 ,323 Hydro e te: e t/Bu 4.300 .1 LiquidHourly Space Velocity, Vol./Hr./ 1.00 0. 95 gf g gg f g F 1 58 7 3 888 Throughput VOL/V01 Ligulitl Hourly Space Velocity, Vol./Hr./ 1 b1 1 08 Balance, Percent by Wt. of Charge: 0

ilydrolcarbon Gases (C1-C3) 917). 3 102.2 Throughputv Vol-[v01 203 Balance, Percent by Wt. of Charge: Sulfur Removed 5 5 lliliydrtacarbon Gases (C1-C5) 1 qlll 99 5 1 Sulfur Removed 1.5 1.6

Liquid Product Inspection: 7

Gravity, API 31.8 36. 4 Total 5 @fifigfififlfl Percent O'04 0'04 Liquid Product Inspection:

ASTM 5 34 0 6 Gravity, AP]: 30-5 34-6 FIA Analysis, t; by v 1 1123, Percent 01J4 ASTM D 1319 i i nh 1159 3.7 1.3

glgigj H 8'? FIA Analysis. Percent by vol.-

ASTM D 1319- Saturates 57 5 85.5 O1 fi 1 6 1 7 Aniline Point, F. A e 6 4 ASTM D 611 117.2 149 9 p s g Distillation, Gas Oil- Aniline ,1

Pgj, o F 346 276 A 'IM D 611. 103.9 137.1

Distillation, Gas Oil End Point, F-.. 642 632 ASTM D 15? 10% jg Over Poirit,F 348 301 2323"" n3 4%? End i t 640 641 70 533 513 424 00 584 572 Recovery, Percent 98. 6 98. 5 70 A N RBesidue, Pelrcellit 115% 11.53 90 vg. 0. lllgS per H10 ecu 6. Avg. No. Aromatic {sings per 0.43 0.10 ggg gg ggf fggw 5 :2 &5 33???? fifiifigk g ggg :6; 8% Average No. Rings per molecule 1. 6i 1. 55 y Average N0. Aromatic Rings per Molecule 0. 56 0. 21 Refractive Index, in, 1. 4872 1 4095 Catalyst Relative Activity .504 898 Catalyst Description Unsullfided CoMoum l I o As shown 1n Table 1, the relative actlvlty for the TotalMetals'Pment 12.54 mm saturation of aromancs for both the supported ndun- Atomic Ratio 0.39 Co: 0.44 00: supported tungsten containing catalysts of this invention Support ,i-gf g },-.3,g',,, increases sharply with an increase in hydrogenation pres- Alumina sure. Table 1 shows that the activity of a 24.48 percent Impregnamn Technique (Vacuum) a s? Dmble sulfided nickel-tungsten catalyst disposed upon a support 7 designated as H-44 alumina and manufactured by the Conditions: Aluminum Company of America increases from a value Hydrogen i 4,100 3,660 of 608 at a h dro enation ressure of 1000 pounds per Avg Temperature F 702 y g p 1 Pressure, .s.i. 'j 3,000 0 square inch gauge to a value of 920 at a hydrogenation ggi Hmlrly space VQL/HYJ 1 03 04 pressure of 2980 pounds per square mch gauge, while Threug'lifiiftj'voliivol: I 4 0 unsupported nickel-tungsten sulfide increases from a Balance Percent by Wt of Charge. value of 689 at a hydrogenation pressure of 1000 pounds iliydrgcarbon Gases '(Gl-Gi) .2 per square inch gauge to a value of 1000 at a hydrogenation pressure of 3020 pounds per square inch gauge. Sulfur Removed 1.9 1. 5

Unsulfided 25.64 percent nickel-tungsten on H-44 Tm] 2. 101-1 alumina has an activity of 589 at a hydrogenation Liquid Produ ct Inspection: pressure of 990 pounds per square inch gauge and an gg g fif g g g9 2 activity of 860 at a hydro enation pressure of 3020 Bromine No. pounds per square inch gauge. Table 1 also shows that gf fg g fllfiggggg g a sulfided 25.4 percent cobalt-tungsten on H-44 alumina ASTM D1319: catal st has an activity of 504 at 1000 pounds per square 1 0 2 1 y 1 inch gauge and that a sulfided 13.4 percent cobalt-tungs- 46.2 47.1 ten on H-42 alumina catalyst has an activity of 898 at Anihne Point F 4311M 5 f 103.3 mm 3000 pounds per square inch gauge. In respect to a Disiilxllsa lloii,]i'irsg oll non-tungsten containing catalyst, on the other hand, an over P int 364 333 unsulfided cobalt-molybdenum on H-44 alumina has an K; 22g 25% activity of 483 at a hydrogenation pressure of 1000 3Q I 472 465 pounds per squareinch and this activity does not increase gg if; 3% with pressure, but is approximately the same (470) at a II 590 57 7 hydrogenation press re of 3000 pounds per square inch %ecodveryi Perce 98.7 98.8 gauge esl ue, ercen 1... 1. Average No. Rings per molecule 1.00 In addition to showing that catalysts containing tungs- "i gg gf f gfi g ffi Per 1019mm 1 32 ten and a group VIII metal exhibit highly superior aro- Catalyst Relative Activit 47o 4 matic saturation activities and that such catalysts are especially sensitive to elevations in pressure, Tablel also shows that a further advantage is achieved by employing nickel as a group VIII metal. For example, sulfided 24.48 .percent nickel-tungsten on alumina has an activity of 608 at 1000 pounds per square inch gauge while sulfided 10.01 percent cobalt-tungsten on alumina exhibits a lower activity of 504 at 1000 pounls per square inch gauge. Again, this same nickel-tungsten catalyst has an activity of 920 at approximately 3000 pounls per square inch gauge while the cobalt-tungsten catalyst exhibits a somewhat lower activity of 898 at 3000 pounds per square inch gauge. Accordingly, it is seen that it is advantageous to employnickel as a group VIII metal in the catalysts of this invention.

It has been found that the'tungsten-containing catalysts of-this invention are most responsive to increases in pressure in the range between 500 and 1000 pounds per square inch gauge. At pressures above 1000 pounds per square inch gauge up to approximately 4000 pounds per square inch gauge these catalysts are somewhat less responsive to pressure changes than in the 500 to 1000 pounds per square inch gauge range. The catalysts of this invention exert a very small activity for aromatic saturation at pressures below 50 pounds-per square inch gauge. Accordingly, when an aromatic-containing charge is treated according to the method of this invention only a minor amount of aromatic saturation will occur at pressures below 500 pounds per square inch gauge. Atsaturation pressures between 500 and 1000 pounds per square inch gauge the greatest portion of the aromatics present will be saturated. Increasing the pressure from 1000 to 3000 or 4000 pounds per square inch gauge will accomplish substantially complete saturation of the aromatics present.

The data in Table 2 illustrate the effect of incremental changes in pressure upon aromatic saturation activity when employing a tungsten-containing catalyst of this invention. The data in Table 2 were obtained by employing a presulfided catalyst comprising 4.9 weight percent nickel and 15.9 weight percent tungsten on H-44 alumina for the saturation of the aromatics present in a light catalytic gas oil at 700 F., 1.0 liquid volume of charge per hour per volume of catalyst and 4000 standard cubic feet of hydrogen per barrel. The charge contained 59.5 percent aromatics. Table 2 indicates the aromatic content of the product of saturation processes carried out on thischarge at the various pressures indicated.

TABLE 2 Effect of pressure on .the saturation activity of a tungsten- Table 2 shows that at 500 pounds per square inch gauge the saturation process resulted in only a 3.2 percent decrease in the percent aromatics present. However, when employing a saturation pressure of 1,000 pounds per square inch gauge the amount of aromatics present decreased 56.3 percent. Increasing the pressure to 2,000, 3,000 and 3,500pounds per square inch gauge only increased the amount of saturation to 57.5, 75.4 and 82.0 percent, respectively. Accordingly, only 3 percent of the aromatics were saturated at pressures up to 500 p.s.i.g. while 53 percent of the aromatics present were saturated at pressures between 500 and 1000 p.s.i.g. Increasing the pressure from 1000 to 3500 p.s.i.g. resulted in the saturation of only an additional 26percent of the aromatics. It is, therefore, seen that the first 500 pounds metals.

of pressure results in the smallest decrease in amount of aromatics per unit of pressure applied, whereas the amount of saturation occurring per unit of pressure applied be tween 500 and 1000 is the. greatest. The amount of satu! ration occurring per unit of pressure is much greater above 1000pounds than below 500 pounds but not as great'as in the interval between 500 and 1000 pounds.

An additional test was made to further illustrate the advantage of employing a tungsten-containing catalyst, In this additional test a non-tungsten containing catalyst comprising 19.7 percent of nickel and molybdenum on H.44 alumina was employed to saturate aromatics in the same feed stock and under the same conditions as indicated for the tests made to obtain the data in Table 2. In this test the feed stock was treated at 1000 p ounds per square inch gauge and the amount of aromatics decreased from 59.5 percent to only 39.1 percent. This is contrasted to the data shown in Table 2 where, when a tungsten-containing catalyst was employed, the amount of aromatics decreased from 59.5 percent to 26.0 percent at a saturation pressure of 1000 pounds per square inch gauge.

The temperature range to be employed in the aromatic saturation processes of this invention is 550 to 850 F. Even at elevated pressures of approximately 3000 p.s.i.g. only minor amounts of aromatics will be saturated at temperatures in the lower portion of this range. When hydrogenation temperatures in the upper portion of this range are employed at elevated pressures near 3000 p.s.i.g. in the presence of the preferred catalysts of this invention, substantially all the aromatics present will be saturated. For example, when employing a nickel-tungsten sulfide catalyst at 3000 p.s.i.g. and a space velocity of 1.0 liquid volume of charge per hour per volume of catalyst for the hydrogenation of the aromatics present in a fluid catalytically cracked furnace oil distillate containing 61.0 percent by volume of aromatics, the total aromatic content was only reduced to 53.5 percent at a hydrogenation temperature of 555 F. However, at a temperature of 715 F. the aromatic content of this charge was reduced from 61.1 percent by volume to only 4.5 percent by volume, the other conditions remaining the same.

Higher temperatures are required when non-tungsten containing catalysts are employed. 'For example, when employing a cobalt-molybdenum alumina catalyst for the saturation of the aromatics in a portion of the same charge under the same reaction conditions the aromatic content of the charge was reduced from 61.1 percent by volume to only 52.5 percent by volume at a hydrogenation temperature of 700 F. Accordingly, it is seen that temperatures of 'at least 550 F. are necessary for the hydrogenative saturation of aromatics in accordance with this invention and that'substantially higher temperatures are required when non-tungsten containing catalysts are employed.

The oxide supported catalysts of this invention should contains 5 to 40 percent metals generally, expressed as pure metals, and preferably between 20 and 28 percent When the supported catalysts of this invention are employed in the sulfided state, they should contain 5 to 40 percent metals generally and preferably the sulfided supported catalysts of this invention should contain 10 to 25 percent metals.

Table 3 presents data illustrating the optimum metals content of nickel-tungsten-alumina catalysts. Table 3 shows the results of tests made with catalysts having varying amounts of nickel-plus-tungsten upon alumina. The tests were made for alumina-supported catalysts having eithernickel and tungsten oxides or nickel and tungsten sulfides. In each case, 1:1 atomic ratios of nickelto-tungsten were used. Both the oxide catalyst and .the sulfide catalyst were tested using a fluid catalytically cracked furnace oil as a charge at a space velocity of 1 liquid VQlllmc of charge per hour per volume of .catalyst of the supporting material is not critical.

activities greater than the unsulfided catalyst.

and at 1000 pounds per square inch gauge and 700 F. with 4000 standard cubic feet of hydrogen per barrel.

TABLE 3 TABLE 4 Eflect of sulfiding temperature on relative activity of nickel-tungsten-alumina Relative activity of nickel-tungsten-alumina catalysts 5 having varying amounts of active metals Unsulflded sqlflded Sulflding Temperature Catalyst Catalyst Weight percent Nickel plus Tungsten at a Oxidcd Sulfided (Reference) 1:1 atomic ratio 1 as- 33 a 15.7 520 605 680: 270 620 a 531 800. 570 678 We have also found that at these increased sulfidin Table 3 indicates that a high saturation activity exists temperatures a critical range of sulfiding time duratioi at a total metals content of about 25 percent of the total exists Within which optimum Promotion is obtained catalysi Wmght expresseq as pure metals m the case of This effect of sulfiding time duration is illustrated in the oxldfid catalyst It is also i ifi that Table 5 The catalyst compositions sulfiding gas comin the case of a sulfided catalyst a high activity is achieved 0 d h d ti 1 d b h 10 in about a 21 wei ht ercent nickel-tun P an y rogen? on con Hons emp oye m o w en amp Y g Y taining the data shown in Table 5 were the same as those sten on alumina catalyst. This shift in maximum activity outlined for the tests illustrated in Table 4 with conversion from the oxide to the sulfide probably occurs because activity improvement brought about by TABLE 5 sulfiding increases as the quantity of active metals on the Effect of sulfiding time on relative activity of nickel catalyst decreases. 25

The aluminasupport employed in the tests illustrated on Table 3 is the H44 support manufactured by the Aluminum Company of America. However, the nature The preferred total metals content for either the oxided or sulfided catalysts of this invention is not limited to any particular support but is representative of the preferred metals content for the catalysts of this invention when employing any suitable porous supporting material having a surface area of 10 to 500 square meters per gram. Carriers within this range possess pore structure characteristics such that the amounts of active metals as specified in this invention may be impregnated upon their surfaces without causing pore plugging which would eliminate a large amount of active catalytic surface and thus cut down the activity of the catalyst.

Although the supported catalysts of this inventioncan be employed in the oxide form, it has been found that sulfiding efiects a significant increase in activity. Certain variables of the sulfiding operation have been found to be critical to the amount of activity increase resulting from sulfiding these catalysts. The variables found to be critical are the composition of the sulfiding gas stream, the sulfiding temperature and the sulfiding time duration.

Table 4 presents a comparison of activity for the saturation of aromatics for catalyst samples sulfided at the temperatures indicated with the activity of an unsulfided catalyst as a reference. All the catalyst samples employed in obtaining the data shown in Table 4 were sulfided for four hours with'a gas having a hydrogen-t0- hydrogen sulfide volume ratio of 12:1 at the various temperatures indicated in the table. The relatively slow conversion rate of the oxides to sulfides meant'that even very low sulfiding gas velocities were satisfactory, such as one volume of sulfiding gas per volume of catalyst per hour. The data in Table 4 were obtained while employing a 20 percent nickel-tungsten on alumina catalyst. A fluid catalytically cracked furnace oil distillate such as that described in Table 1 was employed as a charge during the tests. The hydrogenation conditions were 1000 pounds per square inch gauge, 700 F., 1 liquid volume of charge per hour per volume of catalyst and 4000 standard cubic feet per barrel.

As shown in Table 4, the unsulfided catalyst possessed an activity of 570 while all the catalyst samples sulfided between temperatures of 400 and 800 F. possessed In addition, maximum activities were obtained from the catalyst samples sulfided between-600 and 700 F.

tungsten-alumina Unsulfided Catalyst Catalyst Sulfiding Time-Hours Catalyst Sulfided sulfided (Reference) at 400 F. at 600 F.

Table 5 shows that when a catalyst is sulfided at 400 F., substantially no increase in catalyst activity is achieved by extending the sulfiding time more than one hour. However, when a catalyst is sulfided at 600 F., optimum promotion is achieved by employing a sulfiding time duration of 4 to 12 hours. As shown in Table 5, employing a sulfiding temperature of 600 F. for 4 hours results in approximately a 50 percent greater activity increase due to sulfiding than is realized by sulfiding at 400 F. for 4 hours.

TABLE 6 Eflect of hydrogen to hydrogen sulfide volume ratio on relative activity of nickel-tungste n-alamina Unsulfided Relative Hydrogen-to-Hydrogen Sulfide, Volume Ratio Catalyst Activity (Reference) 0 570 529 2 r Y 570 616 12 r 570' 620 Q t 570 552 It is seen from Table 6 that when a hydrogen-hydrogen sulfide mixture is employed best results are achieved by employing a mixture which has neither too small nor too large a ratio of hydrogen-to-hydrogen sulfide. Table 6 indicates that good results are achieved by employing a hydrogen-to-hydrogen sulfide volume ratio of between approximately 2 and 12. e

An oxided nickel-tungsten-molybdenum-alumina cata! lyst was prepared containing.2.1 percent nickel, 8.9 percent tungsten, and 9.0 percent molybdenum on Alcoa H- 41 alumina, the preparation technique being a double impregnation in which all but 5.0 percent molybdenum was added in the first impregnation. This catalyst possessed an activity of 528 at -a reaction pressure of about 1000 pounds per square inch gauge. After regeneration the catalyst was sulfided at approximately 400 F. for about one hour and the resulting catalyst showed a relative activity of 626 under the same reaction conditions used previously. The same catalyst was sulfided again after regeneration according to the preferred sulfiding conditions of this invention and the resulting catalyst had an activity of 655 under similar reaction conditions. It is seen that operating under the sulfiding conditions of this invention results in an improved catalyst activity.

The catalyst supports of this invention can be impregnated by any suitable method. For example, these supports may be impregnated by either multiple impregnation or single impregnation of the active metals. However, it is preferable that multiple impregnation be employed wherein the tungsten is deposited on the carrier first. It was found that when the tungsten is impregnated upon the carrier before the group VIII metal or metals, a catalyst is produced which has an increased activity as compared to a similar catalyst prepared by simultaneous impregnation. On the other hand, it was found that when the group VIII metal is impregnated upon the carrier before the tungsten, the resulting catalyst has inferior activity as compared to a similar catalyst pr pared by simultaneous impregnation.

Table 7 shows the effect of variations in order of impregnation of active metals on the relative activity of 25 percent 1:1 nickel-tungsten on alumina catalysts. Catalysts having this composition were sulfided under the preferred sulfiding conditions of this invention. They were tested on a fluid catalytically cracked furnace oil distillate charge at a space velocity of one liquid volume per hour per volume of catalyst, at temperature of 700 F., a pressure of 1000 pounds per square inch gauge and a hydrogen rate of 4000 standard cubic feet per barrel.

TABLE 7 Effect of variations in preparation technique on relative Table 7 shows that in the case of the catalyst which was prepared by impregnating nickel and tungsten upon the carrier simultaneously, the relative activity was 608. In the case of the catalyst prepared by impregnating tungsten first, the activity was 634; While in the case of the catalyst prepared by impregnating nickel first the activity was only 592. Therefore, the catalyst prepared by impregnating tungsten first exhibited a higher activity than either of the other two catalysts.

Unsupported metal sulfides, such as nickel-tungstensulfide, are initially somewhat more active for the saturative hydrogenation of aromatic-s than the supported oxided or sulfided catalysts of this invention. However, the unsupported sulfides are only preferable where catalyst regeneration is not required orin applications where catalyst life is unusually long. The reason for this is that the activity of the unsupported catalyst cannot be restored tomore than a small fraction of its initial value of aromatic saturative hydrogenation activity by the usual .catalyst regeneration procedures.

In contrast to the unsupported catalysts which contain large proportions of active metals the supported catalysts f s invention em n on y a ou 20 P IWD act 12 metals yet possess about percent asmuch activity for the saturation of aromatics .and, in addition, maintain their high activity characteristics after repeated regenerations. The data shown in Table 8 show the effect of regeneration on the relative activity of a 20 percent alumina supported nickel-tungsten-oxide catalyst. This catalyst was employed in the hydrogenation treatment of a fluid catalytically cracked furnace oil distillate at 700 F., 1000 pounds per square inch gauge, a space velocity of 1 liquid volume of charge per hour per volume of catalyst and a hydrogenation rate of 4000 standard cubic feet per barrelfor a throughput of 20 volumes of charge per volume of catalyst between each regeneration. The catalyst was regenerated 14 times. Table 8 shows the relative activity of the catalyst for the saturation of aromatics at the outset and after the first and fourteenth regenerations.

TABLE 8 Effect of regeneration on the relative activity of alumina supported nickel-tungsten oxide Number of regenerations Relative Activity The data in Table 8 show that after fourteen regenerations the catalyst experienced an activity loss of only about 4 percent. Since an activity decline of better than 2 percent occurs as a result of one regeneration, the aging due to regeneration of the supported catalysts of this invention consists of a small but sharp initial decline followed by a period of very gradual aging. The regenerative procedure followed in obtaining the data shown in Table 8 consisted in the use of an air-steam mixture upon the catalyst at a temperature of 1050 F. This procedure primarily removes carbon formation from the catalyst surface and pores. Following regeneration, the catalyst is preferably resulfided as described above.

In the preparation of a preferred sulfided nickel-tungsten containing catalyst having nickel and tungsten in a 1:1 atomic ratio and containing 5.42 Weight percent nickel'and 15.88 weight percent tungsten on H-44 alumina support the support which exists initially as a powder is pelleted, broken to 10-20 mesh size and then calcined at 1000 F. for ten hours. An aqueous solution of ammonium meta tungstate is prepared by slurrying finely divided tungstic acid (WO -H O) in Water. Aqueous ammonium hydroxide solution is added to the slurry with stirring and the mixture is then allowed to stand at room temperature for two hours. It is then heated to boiling, cooled, and filtered to remove any insoluble material. Themixture is impregnated upon the support under a vacuum for five minutes and then the impregnated carrier is subjected to atmospheric pressure for ten minutes. Excess liquid is drained from the carrier and it is dried at250 F. for 24 hours followed by calcining at 1000 F. for 10 hours. A solution of nickel nitrate is then prepared by placing nickel nitrate (Ni(NO -6H O) in distilled water. This solution is impregnated upon the carrier under the same conditions as the ammonium meta tungstate impregnation followed by a similar drying and calcining operation. The catalyst is then sulfided by passing a hydrogen-hydrogen sulfide containing mixture, having a. volumetric ratio of hydrogen to hydrogen sulfide of 4, over the catalyst at a temperature of 650 F. for a time. duration of six hours.

The saturation of aromatics according to this invention may be performed concomitantly with other reactions. For example, if aprocess is desired which will result in both aromatic saturation and cracking, the catalysts of this invention may be employed with a cracking ype ppo t A t is P fe able tQ c r y 13 out processes using this catalyst continuously and it is desirable that a space velocity of 0.4 to 20.0 liquid volumes of charge per hour per volume of catalyst be employed.

EXAMPLE 1 A fluid catalytically cracked furnace oil distillate (400-650 F.) was treated in the presence of an unsulfided nickel-tungsten on H-44 alumina catalyst. The catalyst contained 21.30 percent nickel plus tungsten in a 1:1 molal ratio. The hydrogenation conditions were 700 F., 990 pounds per square inch gauge, 4.07 liquid volumes of charge per hour per volume of catalyst, and 2190 standard cubic feet of hydrogen per barrel of charge. Product data were taken after a throughput of 40.7 volumes of charge per volume of catalyst. The following inspection data of charge and product show a decrease in the average number of aromatic rings per molecule from 0.95 to 0.65.

Charge Product AP 24. 3 29.1 Sulfur, Percent 1. 55 0. 08 Average Number Rings per molecule 1. 64 1. 64 Average Number Aromatic Rings per mol l 0. 95 0.65 Refractive Index 1.6169 1. 4942 EXAMPLE 2 Charge Product AP 18. 4 23. 5 Sulfur, Percent 2. 25 0.29 Aniline Point, F 161. 9 184. Carbon Residue, Conrad n, Percen 1. 43 0.25 Vanadium, p.p.m 8. 0. 1 Average No. Rings per molecules 3.10 2. 88 Average No. Aromatic Rings per molecules 1. 37 0. 79

EXAMPLE 3 A Mid Continent vacuum bottoms feed containing 7 percent by volume of crude was treated in the presence of a presulfided nickel-tungsten on alumina catalyst containing 22.8 percent of nickel and tungsten in a 1:1 molal ratio. The hydrogenation conditions were 791 F., 2950 pounds per square inch gauge, 0.52 liquid volumes of charge per hour per volume of catalyst and 4350 standard cubic feet of hydrogen per barrel. The product data was taken after a 45.4 volume throughput. The inspection data for the charge and product is shown below.

Charge Product APT 11.6 19.0 Viscosity, SUV at 130 F 151, 126 1, 368 Sulfur, Percent 0. 92 0. 17 Carbon Residue, Conradson, Percent. 17. 27 8. 48 Insoluble in n-pentane, Percent 10. 04 4. 91 Vanadium. p.p.m 58.0 3. 5 Nickel, ppm 33.0 4. 9

The inspection data shows that the material insoluble in normal pentane decreased from 10.04 percent to 4.91 percent. The material insoluble in n-pentane comprises to a large extent asphaltenes which contain multiple fused aromatic rings and therefore a decrease in the amount of material soluble in n-pentane indicates a corresponddecrease 'in the amounts of aromaticsv present in the EXAMPLE 4.-

A shale oil coker distillate (250-750 F.) was treated in the presence of a presulfided 24.5 percent nickeltungsten on H-44 alumina catalyst containing 24.5 percent nickel and tungsten in a 1:1 molal ratio. The saturation conditions were 774 F., 1000 pounds per square inch gauge, 0.49 liquid volumes of charge per volume of catalyst and 1970 standard cubic feet of hydrogen per barrel. Product data were obtained after a throughput of 17.7 volumes of charge per volume of catalyst. Following are the inspection data of the charge and treated product.

Charge Product APT 25. 3 37. 8 Sulfur, Percent 0. 6S 0. 04 Nitrogen, Percent- 1. 93 0. 44 Oxygen, Percent 1. 38 0. 64 Carbon Residue, Conradson, er 1.04 0. 01 Aniline Point, F 93.0 146. 0

The data shows that the aniline point increased from 93.0 F. to l46.0 F. as a result of the treatment. The aniline point is a measure of the temperature which is required for a mixture of oil sample and aniline to go into solution and an increase in aniline point signifies a decrease in the amount of aromatics present.

EXAMPLE 5 Charge Product APT 25.8 Viscosity, SUV at 210 F- 61 Color, ASTM Union 3. 5 Carbon Residue, Conrads .88 0. 48 Iodine No 11.5 8. 3

The data shows that the iodine number decreased from 11.5 to 8.3 as a result of the treatment. Since iodine number is an indication of the amount of unsatura-tion present, including aromatic unsaturation, a decrease in iodine number is indicative of a decrease in the amount of aromatics present.

Various changes and modifications can be made without departing from the spirit of this invention and the scope thereof as defined in the following claims.

We claim:

1. A process comprising passing an aromatic containing material and hydrogen at a temperature of 550 to 850 F. and a pressure of 500 to 4000 pounds per square inch gauge over a sulfided catalyst comprising between about 15 and 26 percent by weight of tungsten and nickel supported upon alumina, said catalyst prepared by impregnating the alumina with tungsten before impregmating with nickel and sulfiding the metals by passing a mixture containing hydrogen and hydrogen sulfide in a hydrogen-hydrogen sulfide volume ratio between 2:1 and inch gauge over a sulfided catalyst comprising between about 15 and 26 percent by Weight of tungsten and nickel supported upon alumina, said catalyst prepared by impregnating the alumina with tungsten before impregmating withnickel and Sulfiding the metals by passing a mixture containing hydrogen and hydrogen sulfide in a hydrogen-hydrogen sulfide volume ratio between 2:1 and 12:1 over the impregnated metals at a temperature be tween about 500 F. and 750 F. for a time duration of about 2 to 20 hours.

References Cited in thefile of this patent UNITED STATES PATENTS Pier et a1 May 29, 1934 Arnold et a1 June 16, 1953 Ciapetta et a1. -4--- Oct. 18, 1955 Nozaki May 1, 1956 Holm Mar. 5, 1957 Pevere et al. Jan. 28, 1958 UNITED STATES PATENT OFFICE QERTIFICATION 0F CORRECTION January 3 1961 Patent Nor 2367 204 Harold Beuther et al0 It is hereby certified that error appears in the above numbered patent requiring correction and that the said Letters Patent should read as corrected bel Column 7 line 28 for 50- read 500 we Signed and sealed this 30th day of May 1961.

(SEAL) Attest:

ERNEST W. SWIDER I DAVID L. LADD Commissioner of Patents Attesting Qfficer 

1. A PROCESS COMPRISING PASSING AN AROMATIC CONTAINING MATERIAL AND HYDROGEN AT A TEMPERATURE OF 550* TO 850* F. AND A PRESSURE OF 500 TO 4000 POUNDS PER SQUARE INCH GAUGE OVER A SULFIDES CATALYST COMPRISING BETWEEN ABOUT 15 AND 26 PERCENT BY WEIGHT OF TUNGSTEN AND NICKEL SUPPORTED UPON ALUMINA, SAID CATALYST PREPARED BY IMPREGNATING THE ALUMINA WITH TUNGSTEN BEFORE IMPREGNATING WITH NICKEL AND SULFIDING THE METALS BY PASSING A MIXTURE CONTAINING HYDROGEN AND HYDROGEN SULFIDE IN A HYDROGEN-HYDROGEN SULFIDE VOLUME RATIO BETWEEN 2:1 AND 12:1 OVER THE IMPREGNATED METALS AT A TEMPERATURE BETWEEN ABOUT 600* AND 700* F. FOR A TIME DURATION OF ABOUT 4 TO 12 HOURS. 